WO2011082974A1 - Acid sludge adsorption of dnt waste water - Google Patents

Abstract

The invention relates to a method for treating alkaline process waste water from the nitration of aromatic compounds to mono-, di- and trinitroaromatic compounds having a pH value of 7.5 to 13, comprising the steps of a) acidifying the alkaline process waste water by adding concentrated sulfuric acid, which originates from the treatment of the aqueous phase comprising sulfuric acid occurring during nitration, to a pH value below 5, wherein a mixture A is created from a separating organic phase and acidic aqueous phase, b) bringing the mixture A into contact with fresh sludge and c) separating the sludge.

Description

 Acid sludge adsorption of DNT wastewater

 The present invention relates to a process for the treatment of alkaline process waste water from the nitration of aromatic compounds, wherein the alkaline process waste water is acidified by the addition of concentrated waste sulfuric acid, which originates from the processing of the obtained during the nitration aqueous sulfuric acid-containing phase, and the acidified process wastewater is brought into contact with fresh sewage sludge and the sewage sludge is subsequently separated.

Aromatic nitro compounds such as mono- and dinitrotoluene are usually prepared by nitrating the corresponding aromatic compounds by means of a mixture of concentrated nitric acid and concentrated sulfuric acid, called nitrating acid. This produces an organic phase containing the crude product of the nitration, and an aqueous phase containing substantially sulfuric acid, water of reaction and water introduced by the nitrating acid. The nitric acid is almost completely consumed in the nitration.

After separation of the two phases, the aqueous, sulfuric acid-containing phase is mixed again with fresh nitric acid, depending on the technology of the nitration process, or after concentration, and used for nitriding. However, at least a portion of the sulfuric acid must be continuously or discontinuously discharged from the overall process, in order to avoid a concentration of impurities, in particular metallic salts (see also DE 10 143 800 C1). The impurities are, for example, impurities originally contained in the nitric acid and metal compounds which are dissolved out of the reactor and pipe materials under the highly corrosive conditions prevailing in the reaction and the work-up of the aqueous phase.

Concentration of the aqueous sulfuric acid-containing phase resulting from the nitration yields an aqueous distillate of low sulfuric acid content, hereinafter referred to as aqueous distillate of sulfuric acid concentration, and a phase of high sulfuric acid content, hereinafter called concentrated sulfuric acid. The part discharged from the nitriding process The concentrated sulfuric acid is also called waste sulfuric acid in the following.

The crude product of the nitration of aromatic compounds such as benzene, toluene, xylene, chlorobenzene, etc. to the corresponding nitroaromatics usually contains, in addition to the desired nitroaromatics such as nitrobenzene (NB) and dinitrobenzene (DNB), mono- and dinitrotoluene (MNT and DNT), nitrochlorobenzene ( NCB) or nitroxylol also small amounts of mono-, di- and Trinitrophenole (hereinafter called nitrophenols), mono-, di- and Trinitrokresole (hereinafter called nitrocresols) and mono-, di- and Trinitroxylenole (hereinafter called nitroxylenols) and others Hydroxyl groups and nitro groups containing compounds and mono- and Dinitrobenzoesäuren (hereinafter called nitrobenzoic acids).

Aromatic nitro compounds which contain no hydroxyl group or carboxyl group in the molecule are also referred to in the context of the invention as neutral nitroaromatics or neutral nitro bodies. Nitrophenols, nitro cresols, nitroxylenols and nitrobenzoic acids are also summarized below as hydroxynitroaromatics. The crude product from the nitration must be freed from the unwanted by-products before further use. Usually, the by-products are separated by separation of the nitrating acid by multi-stage washing with acidic, alkaline and neutral washing liquid. Whereby usually washed in the given order. The alkaline wash is usually carried out with aqueous sodium hydroxide solution, an aqueous bicarbonate solution or an aqueous ammonia solution. The resulting alkaline process wastewater contains nitrophenols, nitro cresols, nitroxylenols and nitrobenzoic acids in the form of their water-soluble salts of the base used. They are usually present in a concentration of 0.2 to 2.5 wt .-%, based on the alkaline process wastewater. The alkaline process wastewater also contains neutral nitro bodies formed in the nitration, in particular reaction products. In addition, the alkaline wash also contains a large proportion of the resulting inorganic salts. The alkaline process waste water therefore usually contains 500 to 5000 ppm of nitrates, 500 to 5000 ppm of nitrite and a few hundred ppm of sulfate. Neutral nitro bodies are present in the alkaline process water, usually in an amount of several 1000 ppm. The ingredients result in a chemical oxygen demand of 1000 to 20000 mg / L.

The nitrophenols, nitro cresols, nitroxylenols, nitrobenzoic acids and especially their salts are intensely colored and highly toxic to the environment. In addition, the nitrophenols and especially their salts are explosives in higher concentrations or in bulk and must be removed from the wastewater before disposal and disposed of in such a way that they pose no danger to the environment. Since the aromatic nitro compounds have overall bactericidal properties and thus make a biological purification of the waste water impossible, a purification or processing of the wastewater containing aromatic nitro compounds is necessary.

To remove the nitrophenols, nitro cresols, nitroxylenols, nitrobenzoic acids and the neutral nitroaromatics from the process effluents, numerous processes are described in the literature, for example extraction, adsorption, oxidation or thermolysis.

The Encyclopedia of Chemical Technology, Kirk-Othmer, Fourth Edition 1996, Vol. 17, p. 138 describes an extraction process for the separation of nitrobenzene in which the nitrobenzene dissolved in the effluent at the appropriate temperature is removed by extraction with benzene. Benzene, which has dissolved in the water, is removed by stripping before final treatment of the wastewater.

According to US Pat. No. 6,506,948, the aqueous washing phases obtained in the nitration of benzene are extracted directly with toluene, each of the resulting wastewater streams being extracted separately. The toluene stream is then passed into the nitration process and reacted. Nitro cresols and nitrobenzoic acids remain dissolved in the alkaline wastewater stream and must then be separated separately.

The dissolved nitroaromatics and Hydroxynitroaromaten can continue to be removed in an acidic medium by extraction with an organic solvent (Ullmann's Encyclopedia of Industrial Chemistry, 4th Edition, Volume 17, page 386). The hydroxynitroaromatics contained in the alkaline process wastewater can also be converted by acidification into a separating organic phase, which is subsequently separated off. Such a method is described in EP 1 493 730 A1. According to this method, the effluent streams of the neutral and alkaline DNT washes and the sulfuric acid concentration are mixed so that a pH below 5 is established. The effluent of sulfuric acid concentration is the distillate of sulfuric acid concentration having a sulfuric acid concentration of 0.2 to 1% by weight. Upon acidification, an organic phase separates, which is separated. The aqueous phase is fed separately to a further wastewater treatment. In order to prevent crystallization of Hydroxynitroaromaten, the equipment used for the separation and separation must be heated.

EP 0 005 203 describes a thermal process for working up wastewaters containing hydroxynitroaromatics. Here, the waste water containing the Hydroxynitroaromaten in the form of their water-soluble salts, under exclusion of air and oxygen under pressure to temperatures in the range 150 to 500 ° C heated. EP 0 953 546 discloses a thermal process for working up wastewater streams from nitriding plants, in which hydroxynitroaromatics and neutral nitroaromatics can be decomposed simultaneously.

According to WO 2009/027416 A1, prior to the thermolytic treatment of the alkaline effluents from the nitration, the aromatic nitro compounds dissolved therein and containing no hydroxyl groups are removed by extraction.

A disadvantage of the method described above is the often relatively high energy cost of a thermolysis or a Wasserstampfstnppung. If the alkaline process waste water is adjusted to an acidic pH and the organic phase which separates out, which contains hydroxynitroaromatics and nitrobenzoic acids, is separated off only by means of phase separation, the problem of so-called "fouling" occurs precipitated organic phase used pumps and piping systems very quickly by precipitating Linder and crystallizing impurities clog and therefore there is a high need for cleaning.

Furthermore, it is known that in dinitrotoluene production, the dinitrotoluolhaltige, see alkaline sewage by absorption on sewage sludge from most of the dissolved at 70 ° C 2,4- and 2,6-dinitrotoluene before the hydroxynitroaromatics are digested by ozonization , This raises the problem that the nitro cresols can not be converted by the ozonation. In addition, the alkaline wastewater still contains nitrite, which is first oxidized to nitrate by ozone and thus leads to an increased ozone requirement. Thus, at a concentration of 3000 mg / L of nitrite in alkaline process waste water, about 25 to 40% of the ozone is consumed for nitrite oxidation.

Therefore, the object of the present invention is to provide a method which also allows the separation of the nitro cresols from the alkaline process effluents of the nitration of aromatic compound and reduces the energy and expense in the further treatment of the waste water with conventional treatment methods. This object is achieved by the following process for the treatment of alkaline process wastewater from the nitration of aromatic compounds to mono-, di- and Trinitroaromaten having a pH of 7.5 to 13, comprising the steps

 a) Acidification of the alkaline process wastewater by adding concentrated sulfuric acid, which from the workup of the at

Nitration obtained aqueous, sulfuric acid-containing phase, to a pH below 5, wherein a mixture A of separating organic phase and acidic aqueous phase is formed, b) contacting the mixture A with fresh sewage sludge, and c) separating the sewage sludge.

The alkaline process waste water treated with the process according to the invention is greatly depleted of poorly degradable neutral nitro bodies, nitro cresols and nitrobenzoic acids as well as of nitrite. Typically, the percentage reduction in the content of these compounds in an alkaline process treated according to the invention is Zessabwasser from a plant for the production of dinitrotoluene with the inclusion of the dilution by the sewage sludge:

2,4-DNT:

 2,6-DNT:

 Sum (nitro cresols and nitrobenzoic acid)

 Sum (nitrite):

A further advantage of the method according to the invention is that for the acidification of the alkaline process wastewater, the entire amount of waste sulfuric acid produced by acid concentration can be used from the production process of the nitroaromatics. The concentrated sulfuric acid containing by corrosion (pipelines) in the nitration salts comprising Fe, Cr, Ni, Ta, and traces of other heavy metals in the form of their sulfates. Usually, when the salt concentration exceeds 300 ppm, part of the acid is discharged from the process as so-called waste sulfuric acid and must be disposed of or purified by other methods. Thus, the use of this waste sulfuric acid is particularly advantageous because you can save the Entsorgungs- or processing costs. The use of concentrated waste sulfuric acid also leads to the fact that the acidification of the alkaline process wastewater, a large part of the nitrite dissolved in the alkaline process waste water is protonated to nitrous acid, which then disproportionates in nitric acid and nitrogen oxides. The nitrogen oxides can be separated and used, for example, for utilization in nitric acid production. According to a preferred embodiment of the invention, the nitrogen oxides which precipitate on acidification are fed into the nitric acid recovery of the nitriding plant and thus are not lost to the process. The chemical oxygen demand of the wastewater stream treated by the process according to the invention is significantly reduced. By using the concentrated waste sulfuric acid, the amount of process waste water to be purified is not unnecessarily increased, as is the case with the use of dilute acid.

The inventive method is used for processing of alkaline process waste water from the nitration of aromatic compounds. Preferably when the aromatic compounds are benzene, toluene, xylene, chlorobenzene and / or dichlorobenzene.

The alkaline process wastewater obtained from the single-stage or multi-stage washing of the crude product of the nitration with aqueous sodium hydroxide solution, aqueous carbonate or bicarbonate solution or aqueous ammonia solution has a pH of 7.5 to 13, preferably 8, depending on the base used to 10 (measured at 60 ° C) on. According to the invention, the alkaline process waste water is adjusted to a pH below 5, preferably from 0.5 to 3, by adding concentrated sulfuric acid which originates from the workup of the aqueous sulfuric acid-containing phase obtained during the nitration. The pH values in each case refer to the measurement at 60 ° C. Upon acidification of the alkaline process effluent, an organic phase precipitates which contains hydroxynitroaromatics, nitrobenzoic acids and neutral nitro bodies. The acidified, originally alkaline process waste water with the separating organic phase is referred to as mixture A in the context of the invention. The waste sulfuric acid used for the acidification has a concentration of 85 to 95 wt .-%, preferably from 90 to 93 wt .-% to. According to a preferred embodiment, waste sulfuric acid obtained only in the nitration is added for acidification in step a), particularly preferably the entire waste sulfuric acid obtained in the nitration is added in step a). The control of the addition of the concentrated sulfuric acid is advantageously carried out via an online pH measurement.

The alkaline process waste water usually accumulates at a temperature of 55 to 80 ° C. According to the invention, the alkaline process waste water is also acidified at this temperature by adding the concentrated sulfuric acid. The mixing of the concentrated sulfuric acid with the alkaline process wastewater leads to a strong evolution of gas. The separating gas mixture contains NO x, in particular nitrogen monoxide, nitrogen dioxide and dinitrogen monoxide. Was used as an alkaline wash water carbonate and / or bicarbonate solution, the separating gas usually contains 70 to 98.9 vol .-% carbon dioxide and 1, 1 to 30% by volume nitrous gases (NOx). Preferably, the separating gas mixture contains 80 to 98% by volume of carbon dioxide and 2 to 20% by volume of nitrous gases. If the process wastewater contains, instead of alkali carbonate and / or bicarbonate, another base which does not form a gaseous component after acidification, the waste gas consists exclusively of NO _x , usually 47 to 98% nitrogen monoxide, 1 to 47% nitrogen dioxide and 1 to 6 % Nitrous oxide. The NOx-containing waste gases separating off during acidification are preferably separated off and used for the purpose of utilization in the production of nitric acid. Particularly preferably, the separated nitrogen oxides are recycled to the nitric acid recovery of the nitriding plant. The gas mixture is usually fed into the absorption columns of the nitrogen monoxide and nitrogen dioxide absorption of nitric acid recovery of nitration. It is particularly advantageous if the entire gas mixture is recycled directly and without prior separation of CO2 and purification. Fresh sludge is used as absorbent in step b) of the process according to the invention. "Fresh" in this context means that the sewage sludge originates from a sewage treatment plant and has not yet been used for absorption in the process according to the invention or a similar process is active, so long as the remaining portion of the nitrite dissolved in the water can be oxidized to nitrate, in this way an additional positive effect can be achieved, since the nitrite can interfere with a subsequent further treatment, for example in ozone treatment First nitrite must be oxidized to nitrate and so unnecessarily ozone is consumed.

Usually, the sewage sludge used according to the invention as an absorbent has a solids content of 10 to 25 g / l.

According to the invention, the sewage sludge and the mixture A are brought into contact with each other for one minute up to two days, preferably for 2 minutes to 1.5 days.

According to the invention, the sewage sludge and the mixture A are brought into contact with each other by being guided in a common container. More preferably, the mixture A and the sewage sludge are brought into contact in step b) by means of active and / or passive mixing elements. Geeigne- te active and passive mixing elements are known in the art. Under active mixing elements, for example, stirrer, ultrasound, shaker enumerate. For example, channels and internals can be used as static mixing elements.

The alkaline process wastewater usually accumulates at a temperature of 50 to 80 ° C. According to the invention, the alkaline process waste water is also acidified at this temperature by adding the concentrated waste sulfuric acid (step a)). The mixture A initially has a temperature of from 50 to 80.degree. C. in contact with the clarification sludge (step b)). According to the invention, the temperature of the alkaline process wastewater in step a) and of the mixture A at the beginning of step b) is preferably 60 to 75 ° C.

At the beginning of step b), the sewage sludge has a temperature of from 5 to 25 ° C., preferably from 8 to 15 ° C., when brought into contact with the mixture A. This has the advantage that due to the cooling effect and the solids content of the sewage sludge, the organic phase separating off on acidification of the alkaline process wastewater precipitates and absorbs on the sewage sludge. In a preferred embodiment of the invention, the volume ratio of sewage sludge to the mixture A is chosen so that a temperature of 30 ° C or less is established. Due to the strong cooling, the organic compounds, which have a melting point above 30 ° C, precipitate and deposit on the solid components of the sewage sludge. The volume ratio of sewage sludge to mixture A is usually 5: 1 to 1: 2, preferably 3: 1 to 1: 1.

After contacting the sewage sludge with the mixture A in step b), the sewage sludge is separated in step c). This is carried out with the aid of conventional devices known to the person skilled in the art, for example with the aid of decanters or centrifuges; the sewage sludge is preferably separated off with the aid of static separators.

The process according to the invention can be carried out batchwise or continuously. According to the invention, the process is carried out continuously. The method according to the invention is explained in more detail below on the basis of examples:

example 1

400 mL of an alkaline process wastewater from the production of dinitrotoluene at 60 ° C are placed in a 1000 mL stirred tank with gas discharge and internal thermometer. The concentrations of DNT, nitro cresols and nitrobenzoic acids are listed in Table 1. Subsequently, the process waste water is treated with 93% aufkonzentreirter waste sulfuric acid until a pH of 2.5 is reached. The resulting gas mixture is passed through the gas discharge in an adjacent absorber cascade, which is filled with 25% KOH. After gas formation is complete, 400 mL of fresh sewage sludge at 15 ° C from Biology I of the treatment plant of BASF Schwarzheide GmbH are added. The sewage sludge has a dry matter content of 20 g / L. This results in a mixture temperature of 37 ° C. The mixture is then stirred for 30 minutes and transferred to a receiver. After centrifugation, the supernatant is analyzed. The results are also shown in Table 1.

Table 1 :

Component concentration before concentration after quantity reduction

 Treat (treatin [mg / L according to the instructions] [mg / L] M

 2,4-DNT 556 214 62

 2,6-DNT 132 42.0 68

 Nitro cresols, 541 77.6 86

nitrobenzoic Example 2

1000 mL / h of an alkaline process waste water from the production of dinitrotoluene at 60 ° C and continuously 93% concentrated waste sulfuric acid from the acid concentration are continuously controlled in a 500 mL stirred tank (B1) with gas removal to an absorber (A1) and internal thermometer via an inline pH measurement, fed. The pH is adjusted to a value of 0.5. The forming gas mixture is passed through a gas discharge to an absorption column (A1) and thus removed from the process. From the stirred tank (B1) continuously 525 mL of the acidified wastewater of 65 ° C in the container (B2) promoted. In the stirred tank B2 continuously 525 mL / h of the sewage sludge of Biology I of the treatment plant of BASF Schwarzheide GmbH are introduced at 10 ° C. The sewage sludge has a dry matter content of 20 g / L. From the 5000 mL stirred tank B2, which is filled to 70%, a volume flow of 1025 mL / h at 25 ° C is continuously fed into a decanter (D), which after settling the sewage sludge and the adsorbed organic components, a pretreated waste water stream with 21 ° C delivers. The container B2 is connected via an exhaust pipe to the absorption column (A1). The waste water stream from the decanter (D) is analyzed. The concentrations of DNT, nitro cresols and nitrobenzoic acids in the treated and untreated waste waters are compared in Table 2.

Table 2:

Component concentration before concentration after quantity reduction

 Treat (treatin [mg / L according to the instructions] [mg / L] M

 2,4-DNT 556 186 67

 2,6-DNT 132 38.6 71

 Nitro cresols, 541 50.8 91

nitrobenzoic Example 3

Example 3 is carried out as Example 2 with the difference that the pH, which is controlled by the metered addition of waste sulfuric acid from the acid concentration via an in-line measurement, is adjusted to 2.5. The concentration of DNT, nitro cresols and nitrobenzoic acids before and after the treatment according to the invention are compared in Table 3.

Table 3:

Component concentration before concentration after quantity reduction

 Treat (treatin [mg / L according to the instructions] [mg / L] M

 2,4-DNT 556 264 53

 2,6-DNT 132 59.4 55

 Nitrocresols, 541 155 71

nitrobenzoic

Claims

claims A process for the treatment of alkaline process waste water from the nitration of aromatic compounds to mono-, di- and Trinitroaromaten having a pH of 7.5 to 13, comprising the steps of a) acidification of the alkaline process wastewater by adding concentrated sulfuric acid, the from the workup of the obtained during the nitration aqueous, sulfuric acid-containing phase, to a pH below 5, wherein a mixture A of separating organic phase and acidic aqueous phase is formed, b) contacting the mixture A with fresh sewage sludge, and c) separating the sewage sludge. A method according to claim 1, characterized in that the concentrated sulfuric acid used for the acidification has a concentration of 85 to 95 wt .-%, preferably from 90 to 93 wt .-%. A method according to claim 1 or claim 2, characterized in that the total incurred in the nitration waste sulfuric acid is used in step a). Method according to one of claims 1 to 3, characterized in that in step a) the pH is adjusted to 0.5 to 3. 5. The method according to any one of claims 1 to 4, characterized in that the mixture A and the sewage sludge for 1 minute to 2 days are brought into contact with each other. 6. The method according to any one of claims 1 to 5, characterized in that it is benzene, toluene, xylenol, chlorobenzene and / or dichlorobenzene in the aromatic compounds. 7. The method according to any one of claims 1 to 6, characterized in that the alkaline process wastewater in step a) and the mixture A at the beginning of step b) has a temperature of 50 to 80 ° C, preferably from 60 to 75 ° C. Method according to one of claims 1 to 7, characterized in that the sewage sludge at the beginning of step b) has a temperature of 5 to 25 ° C, preferably from 8 to 15 ° C. Method according to one of claims 1 to 8, characterized in that in step b) the volume ratio of sewage sludge to mixture A is chosen so that sets a temperature of 30 ° C or less. Method according to one of claims 1 to 9, characterized in that in step b) the volume ratio of sewage sludge to mixture A at 5: 1 to 1: 2, preferably 3: 1 to 1: 1. 1 1. Method according to one of claims 1 to 10, characterized in that the mixture A and the sewage sludge in step b) are brought into contact by means of active and / or passive mixing elements. 12. The method according to any one of claims 1 to 1 1, characterized in that the acidifying in step a) separating nitrogen oxides are separated and used for recovery in the production of nitric acid. Process according to one of Claims 1 to 12, characterized in that the nitrogen oxides which separate off during the acidification in step a) are separated off and recycled into the nitric acid recovery of the nitriding plant. Method according to one of claims 1 to 13, characterized in that the sewage sludge is separated in step c) in a static separator. 15. The method according to any one of claims 1 to 14, characterized in that the method is carried out in a continuous mode.